EP2470470A1

EP2470470A1 - Method for operating a reactor module for endothermic reactions and reactor having a plurality of such reactor modules

Info

Publication number: EP2470470A1
Application number: EP10795607A
Authority: EP
Inventors: Peter Lutz
Original assignee: Bekon Energy Technologies GmbH and Co KG
Current assignee: Bekon Energy Technologies GmbH and Co KG
Priority date: 2009-08-28
Filing date: 2010-08-27
Publication date: 2012-07-04
Also published as: US20120159848A1; DE102009039276A1; WO2011023177A1

Abstract

The invention relates to a reactor module for endothermic reactions for producing one or more products, a reactor having a plurality of such reactor modules, and a method for operating a reactor module or a reactor. The reactor module comprises a reaction channel (2; 31; 71), which is enclosed by a tubular boundary wall (2a; 31a; 75, 76) and has a first end (3; 32; 72) and a second end (4; 33; 73), at least one first inlet element (3; 35; 72) for introducing at least one reactant into the reaction channel (2; 31; 71), wherein the first inlet element (3; 35; 72) is arranged at the first end (3; 32; 72) of the reaction channel (2; 31; 71), at least one first outlet element (4; 37; 73) for discharging at least one reaction product from the reaction channel (2; 31; 71), wherein the first outlet element (4; 37; 73) is arranged at the second end (4; 33; 73) of the reaction channel (2; 31; 71), and a heat supply device in the form of a porous burner arrangement (10; 50; 60; 80), which is arranged on the outside of the tubular boundary wall (2a; 31a; 75, 76) of the reaction channel (2; 31; 71). Because a porous burner arrangement is used instead of a heat source having catalytic combustion, high reactor performance can be realized at an economically reasonable price. This is a result of the porous burner itself being substantially less expensive than a combustion catalyst.

Description

METHOD FOR OPERATING A REACTOR MODULE FOR ENDOTHERIC REACTIONS AND REACTOR WITH A MULTIPLE OF SUCH REACTOR MODULES

description

The invention relates to a reactor module for endothermic reactions for producing one or more products according to claim 1, a reactor having a plurality of such reactor modules according to claim 15 and a method for operating a reactor module or a reactor according to claim 17.

From US 2006/0122446 A1 a cylindrical reactor module is known which comprises a reaction channel having a first and a second end and an outer side and an inner side. Via a first inlet element at the first end and a second inlet element at the second end, two reaction educts can enter the

Reaction channel can be introduced. Via a first outlet element at the second end and a second outlet element at the first end, reaction products are withdrawn from the reaction channel. Via a heat exchanger, the heat of reaction necessary for an endothermic chemical reaction is coupled into the reaction channel. The necessary for the allothermal steam gasification high heat flux can not be achieved with this known reactor module.

A similar reactor module is also known from US 5,487,876 B1.

From DE 698 35 503 T2 a reactor module for the steam reforming of methanol is known. The reactor module comprises an inlet member for supplying methanol and water vapor, a ring-tubular reaction channel and a

Outlet element for carbon dioxide and hydrogen. On the outside of the

Reaction channel, a porous combustion catalyst is arranged, which burns a portion of the hydrogen produced and in this way gives off heat to the endothermic reforming process in the annular tubular reaction channel. In the innermost tube an exothermic methanation reaction takes place, which also gives off heat in the ring-tubular reaction channel. Also, WO 2008/146052 A1, US 2008/0170975 A1, DE 102 13 891 A1 and German Utility Model G 93 20 711.5 are catalytic

Reforming reactors for the production of hydrogen and methane known.

A disadvantage of the catalytic reforming reactors is that they are not suitable because of the expensive catalyst materials for reactors with high performance.

From EP 1 187 892 B1 a so-called heat pipe reformer is known which comprises a fluidized bed furnace and a fluidized bed gasification chamber. In the fluidized bed gasification chamber is characterized by allothermal steam gasification

Fuel gas produced from carbonaceous feedstocks. The heat required for this purpose is generated in the fluidized bed combustion by means of combustion and over

Heat pipes or heat pipes coupled into the fluidized bed gasification chamber. A disadvantage of a reactor according to EP 1 187892 B1 is that the reaction energy is supplied to the fluidized-bed gasification chamber via heat pipes. This leads to complicated structures and a variety of parts inside the

Fluidized bed gasification chamber, which are flowed around by the fluidized bed, and consequently to a high wear. Therefore, such a reactor must be maintained at regular intervals. In addition, the guided over the heat pipes heat quantity is limited and thus the reaction energy for the allothermal

Steam gasification.

So-called pore burners consist of a temperature-resistant porous material, which is connected to an inlet and an outlet. Into the inlet, a premixed fuel-air mixture is exothermically reacted in a flameless volumetric combustion that stabilizes in many small reactors, the pores. Due to the heat of combustion, the pore body begins to glow. Such a pore burner is known for example from "Gas Heat International (54), 872005".

Further pore burners for different applications and different embodiments are described in DE 10 2005 056 629 B4, DE 103 44 979 A1, DE 10 2004 041 815 A1, DE 10 2006 012 168 A1, DE 20 2005 003 843 U1, US Pat WHERE DE 102 14 468 A1, DE 102006 013445 A1 and EP 0 995 014 B1.

Starting from the US 2006/0122446 A1 or DE 698 35 503 T2, it is therefore an object of the invention to provide a reactor module for endothermic reactions, which has a simple structure and in particular for the production of fuel gas from carbonaceous feedstocks by means of allothermal steam gasification is suitable. It is another object of the invention to provide a reactor which consists of a

Consist of a plurality of such reactor modules and to provide a method for operating such a reactor or reactor module.

This object is achieved with a reactor module according to claim 1, with a reactor according to claim 15 and a method 17.

Characterized in that instead of a heat source with catalytic Verbrennnug a pore burner assembly is used, high reactor power to one

economically reasonable price feasible. This is due to the fact that the pore burner assembly itself is much cheaper than a

Combustion catalyst is. Due to the fact that the pore burner arrangement at the

Outside the reaction channel is arranged, the heat required for the endothermic reaction from the place of their production in the pore body passes directly

Heat conduction and heat radiation through the outer shell of the reactor channel into the reaction channel. The fact that the pore burner arrangement is arranged around the reaction channel, the heat from the reaction channel can no longer escape. The dimensioning of the reaction channel and the pore burner arrangement in the axial and radial directions is chosen so that sufficient heat energy is generated in the pore burner arrangement and transferred to the reaction channel to perform an endothermic chemical reaction in the interior of the reaction channel. The cross section or the diameter of the reaction channel is dimensioned so that over the cross section as uniform temperature distribution is achieved. Depending on the heat output of the pore burner arrangement, this results in a diameter range which still allows this uniform temperature distribution over the cross section of the reaction channel. The cross section of the reaction channel may be circular or even formed as a regular polygon. In each possible embodiment is the

Pore burner arrangement in direct contact with the largest possible proportion of the outside of the reaction channel, so that the largest possible

Heat transfer surface between pore burner assembly reaction channel is given.

Due to the advantageous embodiment of claim 2 and 3, the thermal shielding and isolation of the reaction channel is further improved.

In an advantageous embodiment according to claim 4, it is possible during the operation of the reactor module to introduce at least one reaction educt and / or at least one reaction product via an inlet and / or outlet sluice into the reaction channel or to discharge it from the reaction channel. As a result, a continuous operation of the reactor module is made possible.

In a further advantageous embodiment according to claim 5 is the

Reaction channel arranged vertically. This allows gravity or

thermodynamic effects - e.g. warm gas expands and rises to the top - exploiting at least one reaction educt and / or at least one

Promote reaction product through the reaction channel. By this means, for example, the separation of reaction products, e.g. Gases and liquids or solids.

According to an advantageous embodiment according to claim 6 is via a

Inlet sluice introduced a first Reaktionsedukt in the reaction channel and discharged via an outlet sluice a first reaction product from the reaction channel. Via a second inlet element, a second reaction educt is introduced into the reaction channel and a second reaction product is discharged from the reaction channel via a second outlet element. This is the second one

Inlet member between the inlet lock and the pore burner assembly or disposed between the outlet lock and the pore burner assembly. As well the second outlet element between the inlet lock and the

Pore burner arrangement or between the outlet lock and the

Pore burner assembly may be arranged. In addition, these two inlet and outlet elements can also lead out of the reaction channel or into the reaction channel in the region of the pore burner arrangement. The variability of such

Reactor module allows a variety of endothermic chemical reactions to be carried out.

In addition, the embodiment of the invention according to claim 6 also allows different Reaktionsedukte in countercurrent through the reaction channel to lead The introduced amounts of Reaktionsedukte can be controlled in an advantageous manner so that an optimal implementation of the reaction educts in

Reaction products is achieved.

According to an advantageous embodiment according to claim 7 are in the

Reactor module Fuel gases from carbonaceous feedstock and superheated fuel

Water vapor generated by allothermal steam gasification. As carbonaceous feedstocks, e.g. Coal, tar, tar sand, plastic waste, paper and pulp residues, petrochemical waste, electronic scrap and shredder light fraction, and in particular biogenic feeds, such as e.g. Harvest waste, energy crops (Miskantus) or woodchips or a mixture thereof. The construction of the reactor module advantageously makes it possible for the carbonaceous feedstocks to be introduced into the reaction channel from above through the inlet lock and the superheated steam from below through the inlet in such a way that the carbonaceous feedstocks and the superheated steam are introduced into the reaction channel

flow in opposite directions through the reaction channel. The for the

Production of fuel gases necessary reaction energy is supplied to the reaction channel through the pore burner assembly, wherein the carbonaceous feedstocks and the superheated steam in fuel gas and low-carbon starting materials, hereafter called ashes implemented. The amounts introduced can be dosed in an advantageous manner so that an optimal implementation of

carbonaceous feedstocks and the superheated steam in fuel gas and ash in the reaction channel is achieved. After the chemical reaction it collects Fuel gas in the upper part of the reaction channel and can be discharged via the outlet from the reaction channel. The ash collects in the lower part of the reaction channel and can be discharged from the reaction channel via the outlet lock.

According to an advantageous embodiment according to claim 8, a capacitor is connected downstream of the second outlet element. Through this condenser water vapor contained in the exiting fuel gas is condensed and thus removed from the fuel gas.

In an advantageous embodiment according to claim 9, the

Pore burner assembly a plurality of pore burner elements. One

Pore burner element consists of a fuel inlet for introducing oxygen and fuel, a porous body and a fuel outlet for

Omitting the burnt oxygen-fuel mixture. The fuel can be introduced in liquid or gaseous form or in a mixture thereof in the pore body. A single pore burner element is constructed and dimensioned so that the volumetric combustion over a large part of the

Porous body extends. In the pore burner arrangement around the reaction channel, each individual pore burner element can surround the reaction channel in a ring shape in a first design. The pore burner assembly may also be divided along the circumference into a plurality of pore burner elements, all of them

Pore burner elements together enclose the reaction channel in a second design annular. In addition, the pore burner arrangement can also be formed from a combination of these two designs. A subdivision of the pore burner arrangement into a plurality of pore burner elements makes it possible, for example, to form a temperature gradient within the reaction channel. In addition, maintenance and repair work is simplified because individual pore burner elements are easily replaceable.

In an advantageous embodiment according to claim 10 are at a

Reactor module, the pore burner elements along the reaction channel arranged at a distance from each other. By such an arrangement is advantageously the Increased variability of a reactor module. Because between two adjacent ones

Pore burner elements distances along the reaction channel are present, at least one inlet element and / or outlet element can be arranged at these distances on the reaction channel, whereby at least one Reaktionsedukt and / or reaction product can be introduced into the reaction channel or discharged from the reaction channel. This allows the implementation of a multi-stage chemical reaction in this reactor module. It also makes room for

Provided to provide supply lines for the individual pore burner elements more accessible, which also simplifies maintenance and repair work.

In a further advantageous embodiment according to claim 11 is the

Reaction channel ring-tube-shaped. By at least a first

Pore burner element the outer outside of the ring-tubular

Reaction channel encloses and at least one second pore burner element on the inside of the inner boundary wall outside of the ring-tubular

Reaction channel is arranged, the reaction channel is bordered from two sides by a heat source and therefore it flows heat from two sides in the

Reaction channel. By this configuration, the cross-sectional area of the

The reaction channel can be increased without the "thickness" of the reaction channel influencing the uniformity of the temperature distribution having to be increased

Heat transfer surface between pore burner assembly and reaction channel for given dimensions larger heat flux densities.

The advantageous embodiment according to claim 12, the uniformity of the heat input and the heat distribution is improved in the reaction channel.

The advantageous embodiment of the invention according to claim 13 and 14 allows the production of fuel gas from solid feedstocks. The solid starting materials are portioned, z. B. in the form of pellets, fed above the inlet lock, migrate downwards due to gravity in the reaction channel and the low-carbon solid residues are withdrawn at the lower end via the outlet lock at intervals. The pellets may be provided, for example, by a pelletizer connected upstream of or integrated with the inlet sluice. "

In an advantageous embodiment according to claim 15 forms a plurality of reactor modules from a reactor. This and in particular by the

Parallel connection of the individual reactor modules according to claim 16, a system is provided which allows large-scale production of at least one reaction product.

By the operating method according to claim 17, a part of the fuel gas produced is used as fuel for the pore burner assembly. Therefore, additional fuel for the pore burner assembly must be supplied only in the start-up phase.

Further details, features and advantages of the invention will become apparent from the following description of exemplary embodiments.

Fig. 1 shows a longitudinal section of a first embodiment of the invention.

FIG. 2 shows a cross-section of a first embodiment of the invention along the line A -A in FIG. 1.

Fig. 3 shows a longitudinal section of a second embodiment of the invention. Fig. 4 shows a longitudinal section of a third embodiment of the invention.

Fig. 5 shows a cross section perpendicular to the reaction channel through the

Pore burner arrangement of a fourth embodiment of the invention along the line B - B in Fig. 6.

Fig. 6 shows a longitudinal section of a fourth embodiment of the invention. [first embodiment]

Figs. 1 and 2 show a first embodiment of the invention. A reactor module 1 comprises a reaction channel 2, which is enclosed by a tubular boundary wall 2a, and a first end 3, a second end 4 and a middle one

Section 5 between the first end 3 and the second end 4 has. At the first end 3 at least one Reaktionsedukt is introduced into the reaction channel 2 and at the second end 4 is at least one reaction product from the

Reaction channel 2 deployed. At the middle section 5 encloses a

Pore burner assembly 10 the reaction channel 2 annular. Like from the

Sectional view in Fig. 2 along A - A can be seen in Fig. 1 is the

Pore burner assembly 10 of a first pore burner element 11 and a second pore burner element 21, wherein the two pore burner elements 11, 21 each form half of a cylindrical hollow body divided along the longitudinal axis. Each porous burner element 11, 21 consists of a porous body 12, 22, which has an inner circumferential surface 13, 23, an outer lateral surface 14, 24, a first

Base surface 15, 25 and a second base surface 16, 26 has, as well as a

Fuel inlet 17, 27 and a fuel outlet 18, 28. In the first

Embodiment, the first base 15, 25 of each pore body 12, 22 provided with the fuel inlet 17, 27 for introducing oxygen and a liquid or gaseous fuel, and the second base surface 16, 26 each

Porous body 12, 22 is connected to a fuel outlet 18, 28 to the outlet of

provided burned fuel-oxygen mixture. However, in one or both pore burner elements 11, 21, the fuel inlets 17, 27 of one or both pore bodies 12, 22 also on the second base surface 16, 26 of the pore body 12, 22 and the fuel outlet 18, 28 on the first base surface 15, 25 of Porous body 12, 22 may be arranged.

The inner diameter of each pore burner element 11, 21 is selected so that the inner circumferential surface 13, 23 of each pore body 12, 22, the boundary wall 2a of the reaction channel 2 tightly enclose. By each pore body 12, 22 abut directly on the boundary wall 2a of the reaction channel 2, the heat energy generated in the pore bodies 12, 22 is discharged directly to the reaction channel 2. Thus, a direct heat transfer from the pore burner elements 11, 21 reaches the reaction channel 2. By the transferred heat energy is in the

Reaction channel 2 in an endothermic chemical reaction at least one

Reaction product produced.

[second embodiment]

Fig. 3 shows a second embodiment of the invention. In a reactor module 30 are carbonaceous feedstocks and superheated steam in a

endothermic chemical reaction converted to fuel gas and ash - by allothermic water vapor gasification. The reactor module 30 comprises a

Reaction channel 31, which is enclosed by a tubular boundary wall 31a and is arranged vertically. The reaction channel 31 has an upper end 32, a lower end 33 and a middle portion 34 between the upper end 32 and the lower end 33. At the upper end 32, an inlet lock 35 is arranged, of which only one lock valve 36 is shown in FIG. Between the inlet lock 35 and the central portion 34, a pipe 37 for discharging the fuel gas is arranged, which branches off from the reaction channel 31. At the lower end 33, an outlet lock 38 is arranged, of which only one lock valve 39 is shown in FIG. Between the middle section 34 and the outlet lock 38, a pipeline 40 is arranged for introducing the superheated steam necessary for allothermal steam gasification. In this case, the pipe 40 is formed so that the end piece 41 protrudes in the radial direction in the center of the reaction channel 31 and is bent so that the cross-sectional area of the outlet 42 of the pipe 40 is aligned perpendicular to the axis line of the reaction channel 41 and the outlet 42 to opens up.

At the central portion 34, a pore burner assembly 50 annularly surrounds the reaction channel 31, which consists of four pore burner elements 51. Each individual porous burner element 51 consists of a porous body 52 which is in the form of a cylindrical hollow body with an inner circumferential surface 53, an outer lateral surface 54, a first base surface 55 and a second base surface 56, and a fuel inlet 57 and a fuel outlet 58 identifies. In the present Embodiment, in each pore burner element 51, the fuel inlet 57 is arranged on the first base surface 55 of the pore body 52 and the fuel outlet 58 on the second base surface 56 of the pore body 52, wherein the fuel in each

Porous burner element 51 flows from bottom to top, as indicated by the arrows. However, in a pore burner element 51, the fuel inlet 57 may also be disposed on the second base 56 of the pore body 52 and the fuel outlet 58 on the first base 55 of the pore body 52, with the fuel in the pore burner element 51 flowing downwardly from above (not shown). In addition, in a pore burner arrangement 50, pore burner elements 51 in which the fuel flows in different directions may also be arranged.

The inner diameter of each pore burner element 51 is formed so that the inner circumferential surface 53 of the porous body 52, the tubular boundary wall 31 a of the reaction channel 31 tightly encloses. By each pore body 52 is applied directly to the reaction channel 31, the heat energy generated in each pore body 52 is discharged directly to the reaction channel 31. Thus, direct heat transfer from each pore burner element 51 to the reaction channel 31 is achieved.

In the present embodiment, as shown in FIG. 3, all

Porous burner elements 51 same height and same diameter. However, the pore burner elements 51 may also be different in height and diameter

differ, wherein the diameter of the reaction channel 31 respectively the

Diameter of the respective pore burner element 51 is adjusted.

To generate the fuel gas, the carbonaceous feeds are introduced via the inlet lock 35 in the reaction channel 31 and the overheated

Water vapor introduced through the pipe 40 into the reaction channel 31. The reaction channel 31 can be filled up to the level of the first base surface 55 of the uppermost pore burner element 51. This is the one of all

Pore burner elements 51 generated heat energy supplied to the reaction channel 31. Likewise, the reaction channel 31 can be filled only to the first base 55 of any pore burner element 51 with the carbonaceous feedstocks, wherein advantageously only those pore burner elements 51 for the supply of Heat energy to the reaction channel 31 are used, to the first base 55 of the reaction channel 31 is filled with the carbonaceous feedstocks.

In addition, for the production of the fuel gas, the carbonaceous feeds through the inlet lock 35 and the superheated steam can be introduced through the pipe 40 into the reaction channel 31 so that the

carbonaceous feedstocks and the superheated steam in countercurrent flow through the reaction channel 31. The amounts introduced can be controlled in such a way that optimum conversion of the carbonaceous starting materials and the superheated steam into fuel gas and ash in the reaction channel 31 is achieved. Via the outlet lock 38, the ash located at the lower end 33 of the Reaktioήskanals 31 can be discharged after the chemical reaction.

Third Embodiment

In the following, a third embodiment of the invention will be described with reference to FIG. Here are the same parts as in the previous second

Embodiment provided with the same reference numerals, wherein a re-description of these parts is omitted with reference to the second embodiment.

As can be seen from Fig. 4, the reactor module 30 consists of a

Reaction channel 31, the central portion 34 is annularly enclosed by a pore burner assembly 60. The pore burner assembly 60 consists of a

A plurality, four in the present embodiment of pore burner elements 61. The pore burner elements 61 are, as described in the second embodiment, arranged around the tubular boundary wall 31a of the reaction channel 31.

Each individual porous burner element 61 consists of a porous body 62, which is in the form of a cylindrical hollow body with an inner circumferential surface 63, an outer circumferential surface 64, a first base 65, a second base 66 and a cylindrical central portion 67, and a fuel inlet 68 and a fuel outlet 69 has. In the present embodiment, in each pore burner element 61, the fuel inlet 68 is arranged on the cylindrical middle section 67 of the pore body 62 and the fuel outlet 69 on the first base surface 65 and the second base surface 66 of the pore body 62

Fuel flows through each pore burner element 61 as indicated by the arrows. However, in a pore burner element 61, the fuel inlet 68 may also be connected to the first base 65 and the second base 66 of the porous body 62 and the fuel outlet 69 to the cylindrical central portion 67 of the porous body 62. In addition, pore burner elements 61, in which the fuel flows in different directions, can also be arranged in a pore burner arrangement 60.

Fourth Embodiment

Figures 5 and 6 show a fourth embodiment of the present invention. FIG. 6 shows a longitudinal section of a reactor module 70 and FIG. 5 shows a cross section along B - B in FIG. 6.

The reactor module 70 consists of a reaction channel 71 having an upper end 72, a lower end 73 and a central portion 74 between the upper end 72 and the lower end 73. At the upper end 72 and at the lower end 73 of the reaction channel 71 in the form of a circular cylindrical tube and in the central portion 74 ring-tube-shaped. In the middle section 74, the annular tubular reaction channel 71 is defined by an inner and an outer tubular boundary wall 75 and 76 with a circular cross section. The two tubular boundary walls 75 and 76 have a circular cross-section and are arranged concentrically to one another. In the transition regions 77 and 78 between the upper end 72 and the central portion 74 and the lower end 73 and the central portion 74 of the reaction channel 71 is formed conically.

Arranged in the middle section in direct contact with the inner and outer boundary walls 75 and 76 is a pore burner assembly 80 having first and second outer pore burner elements 82 and 83 and first and second pore burner elements second inner pore burner element 84 and 85. Each of the first outer and the first inner pore burner elements 82 and 84 and the second outer and the second inner pore burner elements 83 and 85 are associated with each other and sandwich the annular tubular central portion 74 of the reaction channel 71. The two outer pore burner elements 82 and 83 have the shape of a hollow cylinder open at the top and at the bottom with a specific wall thickness and circular cross-section. The two inner pore burner elements 84 and 85 are as

Solid cylinder formed with a circular cross-section. Alternatively, the two inner pore burner elements 84 and 85 may be formed as a cylindrical hollow body (not shown). The two inner and outer pore burner elements 84, 85 and 82, 83 are arranged at a distance from each other at the central portion 74 of the reaction channel 71.

The two outer pore burner elements 82 and 83 are as described in the second or third embodiment with a fuel inlet and a

Fuel outlet connected (not shown). As shown in FIG. 6, the first and second inner pore burner elements 84 and 85 are connected to a fuel inlet 90 which passes through the central portion 74 of the reaction channel 71 in the region between the first and second pore burner elements. Also from this area leads a fuel outlet 92 to the outside.

In the fourth embodiment is by the inner and outer

Porous burner element with the ring-tubular reaction channel between a uniform temperature and heat energy distribution inside the reaction channel 71 achieved while at the same time due to the larger contact area between the four porous burner elements 82, 83, 84, 85 and the central portion 74 of the reaction channel 71 more heat energy from the four pore burner elements 82, 83, 84, 85 are transferred to the reaction channel 71. Reactor module reaction channel

limiting wall

first end of 2

second end of 2

middle section of 2 pore burner arrangement first pore burner element pore body of 11

inner lateral surface of 11 outer lateral surface of 11 first base surface of 11 second base surface of 11 fuel inlet of 1 1 fuel outlet of 11 second pore burner element pore body of 21

inner lateral surface of 21 outer lateral surface of 21 first base of 21 second base of 21 fuel inlet of 21 fuel outlet of 21 reactor module

reaction channel

a boundary wall of 31 upper end of 31 lower end of 31 middle section of 31 inlet lock

lock valve

pipeline Auslassschleus

lock valve

pipeline

Tail of 40

Outlet of 40

Porous burner arrangement

Porous burner elements

Porous body of 51

inner lateral surface of 51

outer surface of 51

first floor area of 51

second floor area of 51

Fuel intake of 51

Fuel outlet of 51

Porous burner arrangement

Porous burner elements

porous body

inner lateral surface of 61

outer surface of 61

first floor area of 61

second floor area of 61

cylindrical central portion of 61

Fuel intake of 61

Fuel outlet of 61

reactor module

reaction channel

upper end of 71

lower end of 71

middle section of 71

inner tubular boundary wall of 71 outer tubular boundary wall of 71 upper transition area

lower transition area 80 pore burner arrangement

82 first outer pore burner element

83 second outer pore burner element

84 first inner pore burner element

85 second inner pore burner element

90 fuel intake of 84 and 85

92 fuel outlet of 84 and 84

Claims

claims

1. Reactor module (1; 30; 70) for endothermic reactions to produce

at least one reaction product, with

- a reaction channel (2; 31; 71) which is enclosed by a tubular boundary wall (2a; 31a; 75,76) and has a first end (3; 32; 72) and a second end (4; 33; 73) ;

- at least one first inlet element (3; 35; 72) for introducing at least one reaction educt into the reaction channel (2; 31; 71), the first inlet element (3; 35; 72) being connected to the first end (3; ) of

Reaction channel (2; 31; 71) is arranged;

at least one first outlet element (4; 37; 73) for discharging at least one reaction product from the reaction channel (2; 31; 71), the first outlet element (4; 37; 73) being connected to the second end (4; 33; ) of the reaction channel (2; 31; 71), and

a heat supply device for coupling in the heat necessary for the endothermic reaction, characterized

in that the heat supply device is designed as a pore burner arrangement (10; 50; 60; 80) which is arranged externally on the tubular boundary wall (2a; 31a; 75,76) of the reaction channel (2; 31; 71).

2. Reactor module (1; 30; 70) according to claim 1, characterized in that the pore burner arrangement (10; 50; 60; 80) encloses the reaction channel (2; 31; 71) in an annular manner.

3. Reactor module (1; 30; 70) according to one of the preceding claims, characterized in that the pore burner arrangement (10; 50; 60; 80) is thermally insulated to the outside.

4. Reactor module (30) according to one of the preceding claims, characterized

in that the first inlet element is designed as an inlet lock (35) and / or the first outlet element as an outlet lock (38).

5. Reactor module (1; 30; 70) according to one of the preceding claims, characterized in that the reaction channel (2; 31; 71) is arranged vertically and the first end (3; 32; 72) is at the top and the second end (4; 33; 73) is at the bottom.

6. reactor module (30) according to any one of the preceding claims, characterized

characterized in that a second inlet element (40) is provided for introducing a second reaction educt into the reaction channel (31), and in that a second outlet element (37) for discharging a second one

Reaction product from the reaction channel (31) is provided.

7. reactor module (30) according to claim 4 for the production of fuel gas

carbonaceous, in particular biogenic starting materials by allothermic steam gasification, characterized

^' that the inlet lock (35) for introducing the carbonaceous

Feedstocks in the reaction channel (31) is formed,

that the outlet lock (38) for discharging low-carbon

Product substances from the reaction channel (31) is formed,

in that the second inlet element (40) for introducing superheated

Steam is formed in the reaction channel (31), and

that the second outlet member (37) for discharging the fuel gas from the

Reaction channel (31) is formed.

8. Reactor module (30) according to claim 7, characterized in that the second outlet element (37) is followed by a condenser to separate water vapor from the fuel gas.

9. Reactor module (1; 30; 70) according to one of the preceding claims, characterized

characterized in that the pore burner assembly (10; 50; 60; 80) comprises a plurality of pore burner elements (11, 21; 41; 51; 82, 83, 84, 85).

10. Reactor module (30; 70) according to claim 9, characterized in that the

Pore burner elements (41; 51; 81, 91, 92) are arranged along the reaction channel (31; 71) at a distance from each other.

1 1. Reactor module (70) according to one of the preceding claims 9 to 10, characterized

in

that the reaction channel (71) is at least partially ring-tubular and has an inner tubular boundary wall (75) and an outer tubular boundary wall (76), in that at least one first pore burner element (82, 83) is arranged on the inside of the inner boundary wall (75) on the outside of the reaction channel (71), and

in that at least one second pore burner element (84, 85) on the outside of the outer boundary wall (76) of the annular tubular reaction channel

(71) is arranged.

12. Reactor module (70) according to claim 11, characterized in that the inner and the outer tubular boundary wall (75, 76) have a circular cross-section and are arranged concentrically to one another.

13. Reactor module for producing fuel gas according to one of claims 7 to 12, characterized

in that the reaction channel (31; 71) is arranged vertically and the first end

(32; 72) at the top and a second end (33; 73) at the bottom,

in that the superheated steam inlet element (40) is interposed between the

Pore burner assembly (50; 60) and the outlet lock (38) is formed, and

in that the fuel gas outlet member (37) is interposed between the

Pore burner assembly (50; 60) and the inlet lock (35) is arranged.

14. Reactor module according to claim 13, characterized in that the

Inlet sluice for introduction and the outlet sluice for discharging solids is laid out.

15. Reactor with a plurality of reactor modules (1; 30; 70) according to one of

previous claims.

16. Reactor according to claim 15, characterized in that the individual

Reactor modules (1; 30; 70) are connected in parallel.

17. A method for operating a reactor module (30) according to one of the preceding claims 7 to 14 or a reactor according to claims 15 to 16, characterized in that in the reactor module (30) generated fuel gas of the pore burner assembly (50; 60) as a fuel is supplied.